Apparatus for vaporizing solutions or liquid mixtures and pelleting the residues



y 24, 1951 D. E. MARSHALL 2,561,395

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APPARATUS FOR vAPoRIzI SOLUTIONS okpxqum MIXTURES AND PELLE'IING THE REsIwEs- Original Filed March 16, 1946 6 .Bhoytflhqat 4 ENTOR. I Donald E. Nari/2a.

ATTORNEYJ o. s. MARSHALL 2,561,395 APPARATUS FOR VAPORIZING SOLUTIONS 0R LIQUID MIXTURES AND PELLETING THE RESIDUES July 24, 1951 Original Fild larch 16, 1946 S'Shgqtj-Sli s 7&5

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00): 0/0 t". Nani/9M A TTORNEVJ Patented July 24, 1951 srmrmrus FOR vsromznvc'. sow-nous on mourn MIXTURES AND rms'rmo THE RESIDUES Donald E. Marshall, Summit, N. J.

Original application March 16, 1946, Serial No.

654,996. Divided and this 5, 1948, Serial No. 499

application January '7 Claims. (Cl. 159-4) of these vapors from the solids or product is accomplished in a manner which greatly lessens the destruction of flavors or keeping qualities of the product. Furthermore, the products or separated solids are pelleted and classified to a uniform size, density and structure.

The invention makes possible the known advantages of low temperature, negative pressure dehydration and because of the intensity of the treatment, produces superior results in economy of operation, size of equipment and character of product. The same is true of dehydration at normal pressures conducted in atmospheres of inert non-oxidizing carrier gases.

Another application of this invention is in separating volatile solvents'from chemical solutions being converted to solid particles, such as final steps in the manufacture of plastic molding granules.

Another advantage of this invention to chemi cal processing is that of spreading non-volatile liquid-phase material microscopically thin upon inert or catalytic carrier particles while these particles are in complete gas suspension, virtually untouched by surrounding particles or walls and for a suflicient time to complete a chemical reaction in these liquid-phase films. This may be aided in some cases by the catalytic character of the carrier particle, and in all cases by the large surface area provided by the carrier particle stream. This chemical reaction, for example, may be the re-esterification of fatty-oils with methyl alcohol, thus yielding products of reaction such as methyl ester of fatty-oil and of glycerine which are both readily vaporizable. Then the separation of these vapors from the carrier solid par-' ticles and the fractional condensation of these gaseous products completes the process. Furthermore, such solids as those which discolor fattyoils are co1lected as coating material on the carrier solid particles and these more heavily laden particles are removed for revivification during the recycling of these carrier particles.

With this invention rapid reactions in the liquid-phase can be greatly facilitated by conducting these liquid-phase reactions on the surfaces of carrier particles instead of much slower reactions and less complete actions with liquids in bulk. The type of liquid-phase reactions which are suitable to being promoted by this invention are those which yield vaporizable products.

The invention may be understood from the description in connection with the accompanying drawings in which Fig. 1 is a vertical section through an illustrative sprayer apparatus enclosed within a chamber and having a dust or particle separator in the upper portion of the chamber. Auxiliary units are shown diagrammatically in the lower right hand section of the drawing;

Fig. 2 is an enlarged, fragmental, sectional view of the construction of the lower portion of Fig. 1, again with auxiliary units in diagrammatic form;

Fig. 3 is a section along the line 3-3 of Fig. 2;

Fig. 4 is a side view on an enlarged scale showing a portion of Fig. 1;

Fig. 5 is a view similar to Fig. 1 showing a modiiication;

Fig. 6 is a vertical section of a modified dust or particle separator;

Fig. 7 is a, section along the line 7-1 of Fig. 6;

Fig. 8 is a diagram or flow chart illustrating a way of carrying out the process;

Fig. 9 is a vertical section showing another modification of the structures of Fig. 1 and/or 5.

Fig. 10 is a vertical section of the apparatus shown in Fig. 1 except that the separator of the latter apparatus has been replaced by the separator shown in Fig. 6.

In the drawings, reference character I indicates a chamber that has a sloping bottom wall I. The cylindrical portion of this chamber is jacketed by a jacket 2. An inlet 3 is provided for admitting cooling fluid to this chamber and an outlet 4 is provided for the fluid.

An annular perforated plate 5 that slopes downwardly towards its center is located in the chamber l and is spaced by spacers 5' a short distance from the bottom thereof. Pipes P for air under pressure enter the space between the plate 5 and bottom of container I. The chamber I and jacket 2 are provided with spaced conically-shaped upper portions 6 and 1, respectively. An inlet 8 is provided for the space between the, portions 8 and l, and an outlet 9 is provided therefor.

An inlet I0 is provided for material to be treated. This inlet enters a toroid chamber ii tangentially. A tangential outlet I2 (Fig. 3) is provided from the toroid chamber II. A diverting plate I2 for liquid is provided at the entrance of this outlet I2. A high-pressure liquid pump I5 (Fig. 2) is provided into which the outlet I2 enters. A filter screen I6 is provided'in this outlet. An outlet I1 extends from the pump I5 to 22 and stored or treated in a place not shown.

As an example of such storage or treating place, reference may be made to copending applications Serial Number 624,681, filed October 26, 1945, and Serial Number 610,312, filed August 11, 1945. The lower portion of tube 23, of course, will be connected to such storage or treating space, and suitable means will be provided for conveying the particles through'the tube to the chamber I.

A plurality of upwardly-extending and inward- 1y inclined small tubes 24 (Fig. 2) extend from the bustle 2| into the lower portion of chamber I.

These tubes terminate in nozzle tips 34. A ring 26 integral with the bottom I' is provided around the tubes 29 and has set screws 21 for holding these tubes in assembled relation. The tubes 24 extend through tube 29. A radial horizontal spaces from becoming clogged. Note Fig. 4 which is an enlarged fragmental view of plate 5| showing the projections 62. A vapor outlet is provided above the conical plates I to 54.

A spring 64 is provided with its lower end resting on a bearing on plate 65 that is fixed in position. This spring 64 normally keeps the plates 5I--54 in their uppermost position. Sleeve 61 integral with hollow shaft 51 surrounding shaft 46 is connected to the pulley 58 and a flange at the bottom thereof is pressed upwardly by the spring 64. Magnetically-operated or other sorts of hammers 19 are attached to the supports H on the bracket 12.

In the modification hown in Fig. 5, a chamber is provided with a jacket 15. An upright revoluble tube 11 extends centrally of the chamber 15, and has a conical lower end 11'. A spider 18 is attached to the lower portion of the tube 11. A driving ring gear 19 is attached to the outer ends of spider 18. This ring gear 19 is provided with rollers 89 which rest on a runway 8i that is attached to the inside of the chamber 15. The ring gear 19 i driven by a gear on motor 83 which rests upon a support 84 outside of the jacket 16. A packing gland 85 is provided for the shaft of the motor 83. A scraper 19' fastened to tube 11 revolves to clear space around the lower end of tube 11. I

Centering arms 98 are attached to the chamber 15 for centering the tube 11. A roller bearing 89 is provided between the inner ends ofthe arms 88 and the bearing ring 99 that is attached to inward tubular extension 39 of the chamber II connects with a vertical tubular extension 29 which surrounds the tubes 24. Tubes 24 extend from the bustle 2| almost to the upper ends of the tubes 29 and have tight fits in the lower portion of these tubes 29, leaving spaces 33 around the tubes 24 from the extension 39 to the upper ends of these tubes, thus providing passageways for gases which enter the chamber II. Nozzle tips 34 are provided at the upper ends of the tubes 24. Openings 35 are provided through the tubes 29 to establish communication with the chamber II through the tubular extensions 39 and the spaces 33 between the tubes 24 and 29.

Brackets 38 ,(Fig. 1) are provided on the perforated plates 5 to support a large tube 39 with which the inlet tube 23 for solid particles is concentric.

Abearing 49 is provided for balls 4i and is securely attached to the outside of the tube 39 near its upper end. A slightly conical plate 42, having an opening at its center through which the tube-39 extends, is provided with a ball race near. said opening which rests upon the balls 4|. A deflection plate 43 is rigidly attached by connectors 44 to the conical plate 42. Its lower surface curves upwardly and outwardly from a central point and thence downwardly and outwardlyto its edge. A projection 45 at 'the center of the upper side of the deflection plate 43 is'securely attached to the end of a shaft 46 which is driven by motor 41. pulley 48, belt 49 and pulley 59. The ball 4| and bearing 49 support these parts.

Nested conical plates 5i, 52, 53 and 54 are supported and driven by hollow shaft 51, pulley 58, belt 59, pulley 69 and motor 41. These plates are securely connected together by connectors 6| andthe lower portions of these plates are more nearly horizontal than the upper portions thereof. Projections 62 and 63 are provided along the inclined portions of the lower side of plate 5| and the outside of the tube 11. Radial arms 9| are attached to thetube 11 and carry chains 92 suspended. from vtheir outer ends.

A tangential inlet 94 is provided for material to be treated when it enters separator 95. Outlet tubes 99 for vapors extend from the separator 95 into the tube 11. A valved outlet 91 for liquids extends from the separator 95 to the pump 98 by which these liquids are forced into a ring tube 99 from which the tubes I99 extend into and nearly to the upper ends of the tubes 96 which lead from the upper side of the separator 95, leaving an annular space between the inside of the tubes 96 and the outside of the tubes I99.

Valved outlet 91 is also connected to supply tank. 91' as an alternate source for supplying liquid to pump 98.

Conical plate 86 is revolvably mounted on the open end of tube 11 and studs I98 connect the disk 86, which is a pelleting plate, to the pelton reflector cup I99. A shaft H9 is provided with a pulley III which is driven by a pulley ,2 on a motor II3.

A hollow shaft I I4 is mounted on the shaft I I9. The shaft II4 carries a conically-shaped dust vane assembly consisting of concentric cones II5 that are held in assembled position by spacers A spring H1 is provided to keep this cone as sembled in its uppermost position, but-is permitted to be vibrated when struck by electromagnetic hammers II8. A pulley II9 that is smaller than the pulley III is driven by a pulley I29 of motor II3, which is larger than the pulley H2 Cleanaoenaou' leads from above the dust centrifuge III to a recirculating fan I20, a valve I23 being provided in this pipe. An outlet I30 extends from the fan I20 to a plenum chamber I3I that surrounds the conical bottom of chamber I and tangential inlets I02 with bailies I03 open from the chamber I3l into chamber 15. A pipe 133 for auxiliary fresh air is provided for the fan I29 and a damper I34 is located in this pipe. A branch air line I05 from fan I29 provides elutriating air stream to annular opening I04 surrounding outlet I06 and valve I05 regulates this air. The air lock I04 discharges the products from chamber 15.

A modified dust centrifuge is shown in Figs. 6 and 7, a chamber I35 is provided from which vapors entraining solids or dust are to be exhausted. A casing I36 is provided at the upper portion of the chamber I35. This casing I36 is to be revolved at a high speed. A pulley I31 is provided for revolving the casing I36. A bearing I36 is provided in which the pulley I31 revolves. Cleaning points or projections I30 are provided along the outside of the casing I36 to prevent dust from caking between the chamber I35 and the casing I36.

The revolving casing I36 is provided with attached disks I40 sealed by glands I from the stationary supporting shaft I42. The disks I43 support other disks I40 by studs I55 and are attached by vanes I43 to the casing I36. Revolving disks I40 and I40 provide an air passage I44 leading from inlet I45 to outer periphery of disks I40. A centrifugal air-flow is developed when disk I40 and casing I36 revolve.

Stationary disks I46 and I46 supported on shaft I42 by hubs I41 provide an air by-pass I5I fromouter periphery of revolving disks I40 in the first stage to axial passage I48 which is the entrance to the second stage.

Integral with stationary disks I46 are mounted scrapers I49 arranged to plough collected dust from the inner surface of easing I36. Scrapers I45 are pitched so as to move ploughed dust downwardly from the second stage to the first stage through the openings between the vanes I43. Vanes I43 are also pitched to assist in transfer of dust between plough's I49 of each stage.

Vanes I50 along the outer circumference of the bottom stage also are pitched to propel the dust from the centrifuge down along the wall of chamber I35. The uppermost stage of centrifugal disks I40 deliver through stationary passage I52 to outlet I53. Chamber I35 is sealed from revolving casing I36 by gland I54.

Stationary hollow support I42 provides for shaft 46 which corresponds to shaft 46 in Fig. l. The centrifuge or separator of Figs. 6 and 7 may be described as a multi-stage centrifugal blower, or as bowl centrifuge means. As can be seen, the separator is multi-stage and has, roughly speaking, a bowl shape. As shown in Fig. 10, it may be substituted for the separator shown in the upper portion of chamber I of Fig. 1, where it will act to pump or draw out of the chamber the effluents from the tubes 23 and 30 and any fluidizing gas introduced through the inlets P. It further serves to separate such material into volatile and non-volatile parts, the latter being returned to the chamber, while the volatiles pass out through outlet I53. A belt I80 driven by means not shown serves to drive the pulley member I3Ia, and, of course, the revolvable casing I36a. As will be seen in Fig. 10, the deflector drive shaft 46', which extends through and is rotatable in the stationary tubular shaft I42a, is driven through the pulley a and belt 49a by a motor not shown. Shaft I42a has a lower enlarged portion Ill through which shaft 46' extends and into the lower recessed end of which the projection 45a of revolvable plate or deflector 43a extends. Shaft 46' is connected to the projection 45a. Portions 6a and la of chamber Ia are suitably attached to the outer casing I35a of the separator, as at I82. At its upper end shaft I42a is secured to the housing portion I83, as by being welded, and it may be further supported by the struts or braces I86 situated within the lower part of outlet I53a. Efiluents from chamber Ia pass through inlet I45a, then through the separator, then outwardly through outlet I53a and duct 0a. A wall portion I84 of duct I53a is fastened to a suitable support I65.

All other parts of Fig. 10 correspond to similar parts shown in Figs. 1 and 6.

In the modification shown in Fig. 9 a multiple reflector and tumbling device is illustrated. The lower conical plate I is revolubly supported on draft tube I6I and is attached to the upper conical plate I62 by stay rods I63. The reflector I64 is driven by means not shown and drives the whole assembly through studs I65. An extension shaft I66 integral with drive shaft I61 supports a lower and partial reflecting cup- I60. Openings I69 in the wall of tube I6I provide spaces for reflected material to 'be thrown out on lower conical plate I60 for pelleting.

The operation of the invention in accordance with the several embodiments described above can be performed using liquid input material carrying solids in suspension or solution. The operation will be particularly described in detail in connection with one of the embodiments of the apparatus described above. From this description it will be obvious how the invention can be practiced by using the other apparatus or devices that have been described.

The preparation of the material to be treated may be carried out as shown diagrammatically in Fig. 8. The liquid mixture or solution or compositioai to be treated is introduced by a high pressure liquid diffuser pump which atomizes the material at the diffuser nozzles into the vaporization coil. Heat is added to the input liquid and entraining gas and to the vapors and liquids in the vaporization zone. The vapors are allowed to expand in the vaporization coil and supplement the entraining gas to develop a high-speed input stream to supply inlet I0 (Fig. 1). The input materia1 enters inlet I0 partially in gas phase and partially in liquid-phase in which solids may or may not be suspended.

Toroid chamber II (Fig. 1) serves as a centrifugal separator. The gases or vapors fan out through tubular extensions 30 (Fig. 2) to extension 20 through annular spaces 33 to form a cylindrical envelope around the atomizing nozzle tips 34.

The liquids pass out of outlet I2 through filter I6 to high pressure liquid pump I5 and tubular heat exchanger I8 and bustle 2I thence out through tubes 24. This liquid is atomized by hydraulic pressure induced by pump I 5at nozzle tips 34 inside of the incoming vapor streams.

The vapor and atomized liquid input stream emanating from nozzles 29 and 24 develop an upward jet induced conveyor stream in sparger or draft tube 39 around solid particle input tube 23.

Within this tube 39 the temperature is lowered by flashing of unvaporized input, by the cooling air streams from the elutriator below and by conduction from recycled solid particles so as to congeal the solidiflable material in the input stream. Atomized liquid-phase material coats the recycled solid particles and is carried on the surfaces to assist in nucleation of dust on recycled solid particles and to condition particles for pelleting and forming. Previously formed solid particles from multi-stage process can be introduced through tube 23.

The upward flowing gas and solids stream in tube 39 is reflected by the spinning surface 48 which propels the heavier particles out and down in a counter flowing direction to separate them from th lighter dust and gases.

The reflected solid particles are tumbled on the spinning plate 42 to shape and compact them into pellets. Also, the centrifugal forces propel these pellets out and down the wall of the chamber I forming a barrier between the outer circumference of plate 42 and the chamber wall of the propelled solid particles which bounds the conditioning zone below.

The accumulated bed of reflected solid particles below this barrier is conditioned by cooling and drying gas introduced through inlets P. Violent aeration of this bed of accumulated solid particles is possible for conditioning and classification without serious loss of solids through the barrier of counter flow solids and above, yet allowing the gases to discharge.

The accumulated bed of aerated solids flows or is induced into jet conveyor stream up tube 30 to be re-coated with input liquid or nucleated with smaller particles.

An elutriating gas stream is introduced to the lower end of discharge tube 22 (Fig. 8) and emerges at 22' ,(Fig. 2) to supplement the streams from nozzles 34 passing upwardly through tube 39.

The recycling particles are classified at the bottom of the chamber l. the draft tube 39 and the heavier particles which tend to collect along the surface of the plate fall down counter to the elutriating gas stream from tube 22 and are discharged out through the lower end of tube 22, according to predetermined size balanced with elutriating gas flow.

The lighter are swept up,

k accuses The lighter dust and gases which separate from the reflected solids stream on plate 42 are swept upwardly to dust centrifuge and outlet 0. The spinning vanes 5I54 of the centrifuge develop a friction with escaping gases and induce a centrifugal flow which throws out the entrained dust particles to the outer circumferences of the spaces between vanes 5I54 and deposits their dust on these surfaces by centrifugal force. The hammering mechanism I0 jars the spinning vane assembly 5I-54 in a manner which dislodges the accumulated solids or dust particles and causes them to move by gravity and centrifugal force down and off of the outer periphery of these vanes. These dislodged acsumulations are propelled directly into the recycled main solids stream from plate 42 and become trapped below the barrier of counter flowing solid particles and thence is recycled with the solids stream to be nucleated into larger particles.

The gases induced by an exhausting fan similar to the one shown as I21 imFig. 5 pass through locities of gas flow and hence intesified evapoby virtue of the counter inertia imparted to the separated solids by the mechanical forces of the spinning deflector plates and vanes which develop centrifugal forces several times that of gravity to counteract the entrainment of high velocity gas flow.

In the modification of the invention shown in Fig. 5 the recycled particles are allowed to fall freely below the recycling barrier through a conditioning zone where recycled gases are taken from exhaust through duct I20 and introduced at the bottom of chamber 15 in cycloiiicdirec;

tion through inlets I03 and by baiiles I02. Cooling air or drying air may also be introduced through inlet I33 to properly condition the particles in their fall.

No accumulation of recycled particles is permitted at the bottom of the chamber I5 and the interior walls are swept clean by chain dress 92. The elutriating gas is supplied through duct I05 from blower I29 and to the discharge-duct I05. The proper sized particles fall counter to the elutriating gas and out through the air lock I04.

This modified apparatus and process holds solid particles in free gas suspension throughout most of their travel and develops nucleated particles in a manner similar to the steps in formation of hail stones in nature wherein rain drops are carried in strong up drafts to a cold zone, congeal and fall only to be caught in another up draft where more rain accumulates and solidifies until the hail stones become heavy enough to fall to earth despite the strong upward air current.

Conventional spray-drying'or flash-drying can be practiced in this modified form of apparatus by introducing all of the liquid being treated from supply tank 91' to liquid pump I 5 and heating in tube heat exchange I8 as shown in Fig. 1 and atomizing the whole input at nozzle tips 34 (Fig. 2) enveloped in a cylindrical high velocity hot air stream from tubes 29 having been supplied through duct I0.

A modification of reflecting and forming mechanism is illustrated in Fig. 9 showing how two or more barriers of recycling solids can be obtained by using two or more reflectors I64 and I80. Reflector I68 throws out a portion of the upward input stream and allows the balance to pass to the second reflector I64. Both spinning conical plates I60 and I62 develop a solids stream barrier between their peripheries and the chamber wall I10 through which conditioning gases must pass to escape.

Negative pressure operation can be described by reference to Fig. 8. Input liquid is atomized into .the vaporizing coil and at negative pressure and with the aid of some heat a gas stream is developed without the aid of auxiliary entraining gas. In dther respects the input systems operate the same with the input streams being induced by the exhauster. The reaction zone operates the same way except that higher velocities of gas must make up for lower mass of gas in order to convey the solid particles upwardly.

The exhausted vapors are condensed by cooling and water is removed down a barometric leg. The non-condensible gases pass to an accumulator and out through exhausting ejector or vacuum pump. Conditioning gas is recycled through cooler de-humidifler and is introduced into the bottom of conditioning zone in a manner that conditions falling particles for recycling. Since these non-condensible gases are of low mass at ration is accomplished in a compact chamber negative pressure it is best not to attempt to aerate a bed or these accumulated solid particles. The elutriating gas supply is taken from the recycled non-condensable gas stream and may serve to cool and support larger particles to some extent, but here again the mass of gas must be offset by high velocity which adds a jet to draft tube conveying particles to top of chamber. 3 These high velocity gases will have less tendency to entrain dust from chamber due to larger differential in mass between gas and particle so that the same centrifugal forces will accommodate higher gas velocities of a lighter gas. Since no entrainment gas is introduced and the expanded vapors furnish the gas streams required to convey particles up the draft tube, no additional load is placed on the exhausting system over that required by a. conventional vacuum spray drier, yet the surface exposure and particle formation and small reaction chamber gives many advantages in economy and quality or finished product.

This application is a division or copending application Serial Number 654,996, filed March 16,

In the light of the foregoin description, the following is claimed:

1. Apparatus for producing pelleted solid particles comprising a single chamber; an upstanding tube centrally located in said chamber; means for jetting a stream of gas suspended volatile material and solids into the lower portion of said tube for passage therethrough; rotatable deflecting means adjacent the upper end of said tube for separating solids from volatile material after passage of the same through said tube; rotatable means adjacent said deflecting means. for receiving, pelleting and whirling the separated solids outwardly in the form or a layer of particles concentric with said central tube; a fluidizing zone surrounding said tube and below said layer of whirling particles for receiving said particles; means for fluidizing the particles. in

stream; means for heating and volatilizing a substantial portion or said atomized solution; meansfor separating the unvolatilized portion; means for increasing the hydraulic pressure and temperature of said separated unvolatilized portion; a single chamber having an upstandi'ng sparger tube therein; means for re-combining said unvolatilized portion with theyolatilized portion and the carrier gas and jettingthe recombined stream into the lower portion of said tube for passage therethrough; deflecting means adjacent the upper end of said tube for separating solid particles from volatile material after said fluidizing zone; means for returningfluidized particles from the fluidizing zone to the lower portion of said central tube for contact with said suspended stream; means for removing volatile material from the chamber; and

means for removing solid particles from the chamber.

2. Apparatus for producing compact solid particles from a solution containing said particles dissolved or suspended therein comprising a single chamber; an upstanding rotatable tube in said chamber; means forjetting a. stream of said solution suspended in gaseous material into the lower portion of said tube for passage therethrough; deflecting means adjacent the upper portion of said tube for separating solid particles from volatile material after passage of the same through said tube; rotatable means adjacent said deflecting means 'for receiving and compacting the separated solid particles; a collecting zone adjacent said tube through which the particles may fall freely; means for aerating the freely falling particles in said collecting zone; means for returning the aerated particles from the collecting zone to the lower portion of said tube for contact with said gas jetted stream; means for removing volatile material from the chamber; and means for withdrawing solid particles from the chamber.

3. Apparatus for producing pelleted solid particles from a solution containing said particles dissolved or suspended therein comprising means for atomizing said solution into a carrier gas passage of the same through said tube; rotatable means adjacent said deflecting means for;

receiving, pelleting and whirling the separated solid particles outwardly in the form of a layer; collecting means adjacentisaid tube and below said layer of whirling particles for receiving said particles; means for fluidizing the particles in said collecting means; means for returning fluidized particles from the collecting means to the lower portion of said tube for contact with said jetted, re-combined stream; means for'remov ing volatile material from the chamber; and means for withdrawing solid particles from the chamber.

4. Apparatus for producing pelleted solid particlesirom a solution containing said particles dissolved or suspended therein comprising a chamber; an upstanding sparger tube in said chamber; means for increasing the hydraulic pressure and temperature of said solution; means for atomizing said solution into a. heated carriergas stream to form a solution suspended ingaseous material; means for jetting a stream of said solution suspended in gaseous material into the lower portion of said tube for passage therethrough; deflecting means adjacent the upper end of said tube for separating solid particles from volatile material after passage of the same through said tube; rotatable means adjacent said deflecting means and outside of said tube for receiving, pelleting and whirling the separated solid particles outwardly in the form of a layer; a collecting zone adjacent said tube and below said layer of whirling particles for receiving said particles; means for fluidizing the particles in said collecting zone; means for retuming fluidized particles from the collecting zone to the lower portion of said tube for contact with said stream; means for removing volatile material from the chamber; and means for withdrawing solid particles from the chamber.

5. Apparatus for producing compact solid par- -for receiving said compacted particles; means i for fluidizing the particles in said collecting zone; means for returning fluidized particles from the collecting zone to the lower portionof said tube for contact with said stream; means for removing gaseous material fromthe chamber; multi-stage centrifugal blower and bowl centrifuge means within said single chamber for pumping said gaseous material from the chamber and separating any centrifuged solid particles from said pumped gaseous material and for returning said centrifuged solid particles to said collecting zone; and means for withdrawing the heavier solid particles from the chamber.

6. Apparatus for producing compact solid particles from a solution containing said particles dissolved or suspended therein comprising a single chamber; an upstanding sparger tube in said chamber; means for jetting a stream of said solution suspended in gaseous material into the lower portion of said tube for passage therethrough; deflecting means adjacent the upper end of said tube for separating solid particles from volatile material after passage of the same through said tube; rotatable means adjacent said deflecting means and outside of said tube for receivingand compacting the separated solid particles; a collecting zone adjacent said tube for receiving the separated particles; means for introducing a gaseous fluid to said collecting zone; means for returning the particles from the collecting zone to the lower portion of said tube for contact with said stream; means for removing volatile' material from the chamber; and means for withdrawing solid particles from the chamber.

7. Apparatus for producing compact solid particles from a solution containing said particles dissolved or suspended therein comprising a single chamber; an upstanding sparger tube in said chamber; means for jetting a stream of said solution suspended in gaseous material into the lower portion of said tube for passage therethrough; deflecting means adjacent the up er end of said tube for separating solid particles from volatile material after passage of the same through said tube; rotatable means adjacent said deflecting means and outside of said tube for receiving and compacting the separated solid particles; a collecting zone adjacent said tube for receiving the separated particles; means for introducing a gaseous fluid to said collecting zone; means for returning the particles from the collecting zone to the lower portion of said tube for contact with said stream; means for removing volatile material including gases from the chamber; means for recycling at least a portion of the gases removed from the chamber to the lower portion of said collecting zone; and means forwithdrawing solid particles from the chamber.

DONALD E. MARSHALL.

REFERENCES CITED The following references are of record in the file of this patent:

UNITED STATES PATENTS Number Name Date 1,894,623 Lissman Jan. 17, 1933 1,984,380 Odell ;l Dec. 18, 1934 2,192,515 Crane et al Mar. 15, 1940 2,314,986 Johnson Mar. 30, 1943 2,337,684 Scheineman Dec. 28, 1943 2,347,682 Gunness May 2, 1944 2,381,119 Dill Aug. 7, 1945 2,399,717 Arveson May 7, 1946 

